US5643548A - Drying and separating process and plant - Google Patents

Drying and separating process and plant Download PDF

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Publication number
US5643548A
US5643548A US08/464,810 US46481095A US5643548A US 5643548 A US5643548 A US 5643548A US 46481095 A US46481095 A US 46481095A US 5643548 A US5643548 A US 5643548A
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United States
Prior art keywords
plant
dryer
magnesium sulfite
cracking
exhaust
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Fee Related
Application number
US08/464,810
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English (en)
Inventor
Josef Bammer
Bernhard Blocher
Wolfgang Glaser
Heinz Loquenz
Walter Staufer
Peter Yaldez
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
AE ENERGIETECHNIK GmbH
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Austrian Energy and Environment SGP Waagner Biro GmbH
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Application filed by Austrian Energy and Environment SGP Waagner Biro GmbH filed Critical Austrian Energy and Environment SGP Waagner Biro GmbH
Assigned to AUSTRIAN ENERGY & ENVIRONMENT SGP/WAAGNER-BIRO GMBH reassignment AUSTRIAN ENERGY & ENVIRONMENT SGP/WAAGNER-BIRO GMBH ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: LOQUENZ, HEINZ, YALDEZ, PETER, BAMMER, JOSEF, STAUFER, WALTER, BLOCHER, BERNHARD, GLASER, WOLFGANG
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Assigned to AE ENERGIETECHNIK GMBH reassignment AE ENERGIETECHNIK GMBH ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: AUSTRIAN ENERGY & ENVIRONMENT SGP/WAAGNER-BIRO GMBH
Assigned to AE ENERGIETECHNIK GMBH reassignment AE ENERGIETECHNIK GMBH CHANGE OF ADDRESS Assignors: AE ENERGIETECHNIK GMBH
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/48—Sulfur dioxide; Sulfurous acid
    • C01B17/50—Preparation of sulfur dioxide
    • C01B17/501—Preparation of sulfur dioxide by reduction of sulfur compounds
    • C01B17/506—Preparation of sulfur dioxide by reduction of sulfur compounds of calcium sulfates
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/48—Sulfur dioxide; Sulfurous acid
    • C01B17/50—Preparation of sulfur dioxide
    • C01B17/501—Preparation of sulfur dioxide by reduction of sulfur compounds
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F5/00—Compounds of magnesium
    • C01F5/02—Magnesia
    • C01F5/06—Magnesia by thermal decomposition of magnesium compounds
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the present invention relates to a process for drying and then separating moist salts, such as magnesium sulfite, coming from a wet sulphur dioxide (SO 2 ) absorption plant into MgO, SO 2 and water vapor.
  • moist magnesium sulfite is dried in a dryer and then passed through a solid materials lock to a separating plant which is separated from the dryer thereby.
  • a gaseous component of SO 2 separated from the magnesium sulfite in the separating plant is used to heat combustion air needed to heat the separating plant and another gaseous stream of exhaust gas escaping from the separating plant is used to heat the dryer.
  • the present invention also relates to an installation for drying and subsequently separating moist salts such as magnesium sulfite coming from a wet SO 2 absorption plant.
  • a salt such as MgSO 3 or Mg(HSO 3 ) 2 develops in a moist or dissolved state. If this salt is separated for reclamation of the components, acid vapors such as SO 2 -water vapor mixtures develop at high temperatures, and such mixtures are highly corrosive during cooling (condensation of the water vapor) and also operate to thin the acid to be obtained or cause the acid to be combined with the corrosion products. This hinders heat recovery, equipment costs increase and productive power drops. Moreover, the corrosive vapors adversely affect the equipment, so that maintenance expenses or replacement expenses further lower the productive power of the chemical reclamation plant. Thus, the overall presence of SO 2 -water vapor mixtures is very problematic in salt reclamation operations.
  • German Patent Publication No. DE 1 199 74 describes a similar process for obtaining sulphur dioxide by using zinc oxide whereby the main problem is to avoid sulphatizing the zinc in the separation reactor. This problem does not occur in the present invention wherein the main difficulty sought to be overcome is the corrosion of the elements of the separation plant due to the presence of sulphur dioxide-water vapor mixtures and the high heat requirements of the plant.
  • SO 2 sulphur dioxide
  • H 2 O steam
  • a pure (dry) acid anhydride (SO 2 ) is formed.
  • the components affected by the pure (dry) acid anhydride (SO 2 ) are less subject to corrosion than if contacted with SO 2 -water vapor mixtures, so that the productive power of the plant is unexpectedly high.
  • the dryer in which the moist salts (MgSO 3 ) are situated is heated to a temperature of about 200° C. and preferably more than 200° C. by the circulation of a portion of an exhaust vapor stream of the dryer through a system of conduits.
  • the portion of the exhaust vapor stream of the dryer is heated as a result of heat exchange with an exhaust gas being discharged from the separation plant and directed through a system of conduits, i.e., by passing the streams through separated tubes of a heat exchanger.
  • SO 2 with a purity value of about 70%, and preferably more than 70% is produced and MgO in the form of dust is produced (in the separating plant) for feedback into an SO 2 absorption plant.
  • the separating plant is made in form of an indirectly heated rotary tubular kiln and the dryer is made in form of a directly heated rotary tubular kiln or in form of a fluidized bed dryer, in particular with heating surfaces dipping into the fluidized bed.
  • a feedback channel or other conduit is connected thermically to the separating plant, i.e., via a heat exchanger, for part of the stream of the water/steam mixture produced in the dryer.
  • the drying and separating plant is incorporated thermically and in manufacture into an SO 2 absorption plant, in particular for the reclamation of the boiling acid of a cellulose production.
  • the dryer and the separating plant may also be incorporated into a SO 2 absorption plant of a caloric power plant, the separated SO 2 being obtained in a liquefied form.
  • the installation may include a dust collection apparatus through which the partial exhaust vapor stream from the dryer is directed prior to its passage through the heat exchanger.
  • This dust collection apparatus has a dust outlet side at which dust collects and an exhaust vapor side. The dust collected at the dust outlet side is directed into the dryer. A portion of exhaust vapor from the exhaust vapor side is passed to an exhaust vapor utilization system and another portion of exhaust vapor is directed to the heat exchanger and therefrom into the dryer.
  • the separating plant has an exhaust gas side which is connected to the heat exchanger.
  • such a plant may have a liquid circuit and sludge side at which magnesium sulfite is accumulated and which is connected to the dryer.
  • the separating plant has a solid material side at which magnesium oxide is accumulated and which is connected to a liquid circuit of the SO 2 absorption plant.
  • the SO 2 absorption plant may include a compressor and a steam producing unit having a steam/air pre-heater. A portion of the exhaust vapor stream from the dryer which is not passed through the heat exchanger is directed through this compressor to the steam/air pre-warmer.
  • the SO 2 absorption plant may comprise a steam producing unit having a combustion chamber whereby the exhaust stream from the separating plant is incorporated into the combustion chamber in the form of an oxygen carrier before the SO 2 absorption plant.
  • the invention makes it possible to effect a nearly residue-free desulfurization of caloric power plant exhaust gases in that the metal oxide (MgO) is reused for absorption and develops in form of SO 2 and possible CO 2 in a salable state.
  • the invention also makes it possible to use dolomite, essentially CaMg(CO 3 ) 2 , as the absorption means for the economic production of pure MgO.
  • the pure calcium sulfite which develops can be utilized or deposited, and the acid anhydride would be CO 2 , with the advantage that through the obtaining of the MgO share, the entire calcium sulfite quantity is reduced to approximately 50% of what it was in SO 2 absorption plants operating on calcium base, so that the capacity of the gypsum market is not exceeded.
  • Another application of the invention is to obtain pure CO 2 from combustion exhaust gases on basis of calcium, in which the burning of the calcium takes place outside the combustion and the CaO or Ca(OH 2 ) is used for the absorption of the CO 2 -containing, practically SO 2 -free exhaust gas.
  • the developing calcium slurry (CaCO 3 ) is then dried and the water of crystallization is driven out for the major part, whereupon the water-free CaCO 3 is separated thermically and the calcium oxide is again fed to the absorption process.
  • FIG. 1 is an illustration of a first embodiment of the invention.
  • FIG. 2 is an illustration of a second embodiment of the invention.
  • a salt produced in a salt production plant is introduced into a dryer 2 in a moist state, i.e., with adhering water and with the crystal structure of incorporated water (water of crystallization), whereby the water contents are transferred completely to the heating medium as a result of the heating in the dryer to a temperature greater than or equal to about 200° C.
  • the water of crystallization is necessary to maintain the crystalline properties of the salt but is capable of being removed therefrom by sufficient heat which is present in the dryer 2.
  • the salt is MgSO 3 .XH 2 O and the addition of H 2 O reflects the moist condition of its entry into dryer 2.
  • the dryer 2 When the dryer 2 is in the form of a rotary tubular kiln, a significant quantity of dust is carried into the dryer 2 with the heating medium (exhaust vapor as explained below), i.e., from the outlet end of the dryer 2 as shown in the drawing with respect to the inlet of the salt.
  • the dust is removed from the dryer into a conduit, i.e., from the inlet end of the dryer 2, and is returned to the dryer 2 after passing through a dust collection apparatus 4, e.g., a cyclone, having been discharged from a dust outlet side thereof.
  • a dust collection apparatus 4 e.g., a cyclone
  • the resultant quantity of dust is returned to the dryer 2 with the salt.
  • the exhaust vapor is thus removed from the dryer 2, and directed through the duct collection apparatus 4 to remove dust therefrom, and then a portion thereof is directed back into the outlet end of the dryer 2 after it has been heated in a heat exchanger 5.
  • the acid anhydride is SO 2 and the metal oxide is MgO.
  • the gas/solid material separation is relatively simple.
  • the separating plant is heated indirectly, and to a temperature preferably in the vicinity of about 700° C., so that the heating gas does not come into contact with the medium, the dried salt, to be separated.
  • Hot exhaust gas is directed through tubing and conduits from the separating plant 1 in a circuit.
  • a portion of the exhaust gas is heated in a combustion plant 12, after it has passed through at least heat exchanger 5 and lost some of its heat, so that upon its departure from the combustion plant 12 and entry into the separating plant 1, the temperature of the exhaust gas is slightly above the separating temperature, i.e., the temperature at which the separating plant is operating.
  • the recirculation of exhaust gas leads to a reduction of NO x contents therein.
  • the separating plant 1 exhaust gas is first cooled in the heat exchanger 5, wherein its heat is transferred to the exhaust vapor for the dryer 2, and thereafter the separating plant exhaust gas flows into an air heater 13.
  • air heater 13 fresh air is introduced and is preheated with the intent to deliver the heated air to the combustion plant 12 and, if necessary, to a steam producing unit 9.
  • This stream of fresh air is further heated in a second air heater 14, prior to the combustion unit 12 and possible steam producing unit 9.
  • the acid anhydride coming out of the separating unit 1, mainly SO 2 transfers its heat to this stream of fresh air and is thus cooled down from the separating temperature.
  • the cooled separating plant exhaust gas after it has passed through heat exchanger 5 and air heater 13, contains a relative large amount of heat and can therefore be used as a pre-heated oxygen carrier, when added to a quantity of oxygen, in the steam producing unit 9, e.g., of a lye burning plant 16 in order to increase the heat turnover.
  • the steam producing unit 9 is heated by fuel 10 introduced therein which may be spent lye.
  • Air from the second air heater 14 is further heated in a steam/air pre-heater 8, whereby the steam in the pre-heater 8 is the excess exhaust vapor from the dryer 2 (that portion which did not recirculate through the heat exchanger 5 and the dryer 2) which is compressed in a compressor 7 prior to its passage through the pre-heater 8.
  • part of the combustion air being directed into and through the pre-heater 8 can be fed via the air pre-heaters 13 and 14.
  • the steam producing unit 9 can be an oil-fired power plant boiler the exhaust gas of which contains SO 2 .
  • SO 2 is absorbed by a metal oxide foam, e.g., MgO, with a view toward forming the salt or sulphate MgSO 3 , whereby the salt MgSO 3 accumulates in the form of an insoluble bottom sediment.
  • MgO metal oxide foam
  • This MgSO 3 -containing sediment may then be introduced in form of a water/salt mixture into the dryer 2, preferably after at least an initial drying process.
  • the use of a power plant boiler offers the advantage that the absorption medium is produced in the plant itself and that the contaminant SO 2 occurs in a practically pure and highly concentrated form, i.e., is salable.
  • the spent cellulose lye is used as the fuel 10 and the exhaust gas contains a relatively large amount of SO 2 , so that a bisulfite production plant 11 can be intercalated or interposed between an SO 2 absorption plant 6 and the steam producing unit 9, through which the magnesium bisulfite which is needed in the cellulose process is produced.
  • the remaining SO 2 can then be absorbed or recovered from the exhaust gas in the manner mentioned above, or can be made available for the cellulose process.
  • the plant furthermore makes it possible to obtain CO 2 from the SO 2 -free exhaust gases of power plant boiler installations, whereby calcium or CaO is used or recycled as the absorption medium, for example.
  • the exhaust gas coming from the separating plant 1 which has given up part of its heat to the heat exchanger 5 or to the air heater 13 can now be mixed in the combustion chamber or into the exhaust gas before the flue, depending on the remaining heat contained in the steam producing unit 9, in particular in case of increased oxygen 5 contents, or also before the sulfite production unit 15, if the quantity of SO 2 is high.
  • an SO 2 absorption plant 6 is an installation in which the SO 2 content of a fluegas is absorbed by an absorbent, in this case either CaO or MgO.
  • the flue gas comes from a steam generator 9 fired by coal or oil or another sulfur-containing fuel, preferably by "used boiling acid" of a cellulose production process containing lignin and other organic substances.
  • the steam generator 9 is part of a caloric power plant or, in the case of a cellulose production operation, [art of the recovery plant for the new boiling acid.
  • the fluegas must not contain SO 2 impurities.
  • an SO 2 absorption plant is required.
  • the absorption plant delivers MgSO 3 or CaSO 3 which must be split into MgO or CaO and SO 2 , the MgO and CaO being reusable in the absorption plant and the SO 2 salable in liquid form.
  • the installation can furthermore be also used for pure MgO reclamation from Dolomite, with calcium sulfite being produced as a waste material if it cannot be used for gypsum production.
  • pure MgO reclamation from Dolomite, with calcium sulfite being produced as a waste material if it cannot be used for gypsum production.
  • only part of the SO 2 can then be reclaimed from the exhaust gas of the steam producing unit 9.
  • a fluidized bed dryer 17 may be utilized.
  • a fluidized bed dryer 17 includes heating surfaces and in a similar manner to the embodiment described in FIG. 1, a moist salt is introduced therein.
  • Exhaust vapor is directed from the fluidized bed dryer 2 to a zylon separator 18, the gas therefrom is removed as exhaust (a portion of which is later reheated and redirected through the fluidized bed dryer 2) while the solid material is passed via the solid materials lock 3 to the separating plant 1.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Treating Waste Gases (AREA)
  • Drying Of Gases (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Gas Separation By Absorption (AREA)
US08/464,810 1992-12-04 1993-12-02 Drying and separating process and plant Expired - Fee Related US5643548A (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
AT0239992A AT397929B (de) 1992-12-04 1992-12-04 Verfahren und anlage zur trocknung und anschliessenden spaltung
AT2399/92 1992-12-04
PCT/AT1993/000182 WO1994013580A1 (de) 1992-12-04 1993-12-02 Verfahren und anlage zur trocknung und anschliessender spaltung

Publications (1)

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US5643548A true US5643548A (en) 1997-07-01

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US08/464,810 Expired - Fee Related US5643548A (en) 1992-12-04 1993-12-02 Drying and separating process and plant

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US (1) US5643548A (es)
EP (1) EP0672020B1 (es)
JP (1) JPH08504162A (es)
AT (1) AT397929B (es)
CZ (1) CZ139995A3 (es)
DE (1) DE59302395D1 (es)
DK (1) DK0672020T3 (es)
ES (1) ES2088699T3 (es)
FI (1) FI952526A0 (es)
GR (1) GR3020556T3 (es)
NO (1) NO952097L (es)
WO (1) WO1994013580A1 (es)
ZA (1) ZA939079B (es)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7895769B2 (en) * 2003-05-26 2011-03-01 Khd Humboldt Wedag Gmbh Method and a plant for thermally drying wet ground raw meal
US20110140459A1 (en) * 2008-06-05 2011-06-16 Cemex Research Group Ag Enhanced electricity cogeneration in cement clinker production
US10914519B2 (en) * 2013-05-07 2021-02-09 Andritz Technology And Asset Management Gmbh Method for producing salts with a reduced water of crystallisation content

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2009234829A (ja) * 2008-03-26 2009-10-15 Bio Coke Lab Co Ltd 水酸化マグネシウムリサイクル方法及び水酸化マグネシウムリサイクル装置
CN107648989A (zh) * 2017-09-22 2018-02-02 华电电力科学研究院 一种高品质余热回收防腐蚀装置及其工作方法

Citations (17)

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US3156455A (en) * 1961-12-07 1964-11-10 Holo Flite Int Inc Methods of effecting heat exchange and heat transfer devices therefor
DE1199741B (de) * 1962-12-12 1965-09-02 Metallgesellschaft Ag Verfahren zur thermischen Spaltung des bei der Reinigung schwefeldioxydhaltiger Abgase anfallenden Zinksulfits in Zinkoxyd und Schwefeldioxyd
US3437330A (en) * 1965-11-26 1969-04-08 Conzinc Riotinto Ltd Continuous production of alpha plaster
US3607033A (en) * 1969-01-27 1971-09-21 Chemical Construction Corp Recovery of sulfur dioxide from waste gas streams
US3607068A (en) * 1968-07-22 1971-09-21 Elcor Chem Corp Sulfur recovery process
FR2094193A3 (es) * 1970-06-11 1972-02-04 Chemical Construction Corp
US3826812A (en) * 1971-10-22 1974-07-30 Basic Inc Treatment of flue gases and the like
FR2264878A1 (es) * 1974-03-22 1975-10-17 Ver Refractories Ltd
AT347236B (de) * 1977-06-08 1978-12-11 Waagner Biro Ag Verfahren zur rueckgewinnung des magnesiumbi- sulfits aus dem agbasen eines laugenverbrennungskessels
US4247518A (en) * 1975-05-23 1981-01-27 Rhone-Poulenc Industries Apparatus for the thermal conversion of gypsum
US4455285A (en) * 1978-08-08 1984-06-19 Watkins David W Heat treatment of material
US4569831A (en) * 1985-04-01 1986-02-11 Fuller Company Process and apparatus for calcining gypsum
EP0331294A2 (en) * 1988-02-08 1989-09-06 BPB INDUSTRIES public limited company Improvements in method and apparatus for calcination
US4990319A (en) * 1987-09-15 1991-02-05 Kuraray Co., Ltd. Process for producing ammonia and sulfur dioxide
WO1992016468A1 (de) * 1991-03-25 1992-10-01 Promineral Gesellschaft Zur Verwendung Von Mineralstoffen Mbh Verfahren zum kalzinieren von feuchtem gips
US5169444A (en) * 1986-02-20 1992-12-08 Gebruder Knauf Westdeutsche Gipswerke Kg Process for preparing calcium sulfate anhydrite
US5169617A (en) * 1990-02-19 1992-12-08 Ruedersdorfer Zement Gmbh Method of treating produced gypsum

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US3653823A (en) * 1970-02-27 1972-04-04 Chemical Construction Corp Removal of sulfur dioxide from gas streams
DE3701660A1 (de) * 1987-01-21 1988-08-04 Vysoka Skola Chem Tech Verfahren zur entschwefelung von abgasen und vorrichtung zur durchfuehrung dieses verfahrens
DE3830390C1 (en) * 1988-09-07 1989-12-07 Deutsche Babcock Anlagen Ag, 4200 Oberhausen, De Regenerative SO2 flue gas purification

Patent Citations (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3156455A (en) * 1961-12-07 1964-11-10 Holo Flite Int Inc Methods of effecting heat exchange and heat transfer devices therefor
DE1199741B (de) * 1962-12-12 1965-09-02 Metallgesellschaft Ag Verfahren zur thermischen Spaltung des bei der Reinigung schwefeldioxydhaltiger Abgase anfallenden Zinksulfits in Zinkoxyd und Schwefeldioxyd
US3437330A (en) * 1965-11-26 1969-04-08 Conzinc Riotinto Ltd Continuous production of alpha plaster
US3607068A (en) * 1968-07-22 1971-09-21 Elcor Chem Corp Sulfur recovery process
US3607033A (en) * 1969-01-27 1971-09-21 Chemical Construction Corp Recovery of sulfur dioxide from waste gas streams
FR2094193A3 (es) * 1970-06-11 1972-02-04 Chemical Construction Corp
US3826812A (en) * 1971-10-22 1974-07-30 Basic Inc Treatment of flue gases and the like
FR2264878A1 (es) * 1974-03-22 1975-10-17 Ver Refractories Ltd
US4247518A (en) * 1975-05-23 1981-01-27 Rhone-Poulenc Industries Apparatus for the thermal conversion of gypsum
AT347236B (de) * 1977-06-08 1978-12-11 Waagner Biro Ag Verfahren zur rueckgewinnung des magnesiumbi- sulfits aus dem agbasen eines laugenverbrennungskessels
US4455285A (en) * 1978-08-08 1984-06-19 Watkins David W Heat treatment of material
US4569831A (en) * 1985-04-01 1986-02-11 Fuller Company Process and apparatus for calcining gypsum
US5169444A (en) * 1986-02-20 1992-12-08 Gebruder Knauf Westdeutsche Gipswerke Kg Process for preparing calcium sulfate anhydrite
US4990319A (en) * 1987-09-15 1991-02-05 Kuraray Co., Ltd. Process for producing ammonia and sulfur dioxide
EP0331294A2 (en) * 1988-02-08 1989-09-06 BPB INDUSTRIES public limited company Improvements in method and apparatus for calcination
US5169617A (en) * 1990-02-19 1992-12-08 Ruedersdorfer Zement Gmbh Method of treating produced gypsum
WO1992016468A1 (de) * 1991-03-25 1992-10-01 Promineral Gesellschaft Zur Verwendung Von Mineralstoffen Mbh Verfahren zum kalzinieren von feuchtem gips
US5437850A (en) * 1991-03-25 1995-08-01 Sulzer-Escher Wyss Gmbh Method for calcining moist gypsum

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7895769B2 (en) * 2003-05-26 2011-03-01 Khd Humboldt Wedag Gmbh Method and a plant for thermally drying wet ground raw meal
US20110140459A1 (en) * 2008-06-05 2011-06-16 Cemex Research Group Ag Enhanced electricity cogeneration in cement clinker production
US8997489B2 (en) * 2008-06-05 2015-04-07 Cemex Research Group Ag Enhanced electricity cogeneration in cement clinker production
US10914519B2 (en) * 2013-05-07 2021-02-09 Andritz Technology And Asset Management Gmbh Method for producing salts with a reduced water of crystallisation content

Also Published As

Publication number Publication date
FI952526A (fi) 1995-05-24
NO952097D0 (no) 1995-05-29
JPH08504162A (ja) 1996-05-07
GR3020556T3 (en) 1996-10-31
ZA939079B (en) 1994-08-05
FI952526A0 (fi) 1995-05-24
EP0672020A1 (de) 1995-09-20
ES2088699T3 (es) 1996-08-16
AT397929B (de) 1994-08-25
ATA239992A (de) 1993-12-15
EP0672020B1 (de) 1996-04-24
CZ139995A3 (en) 1996-01-17
DE59302395D1 (de) 1996-05-30
DK0672020T3 (da) 1996-07-29
WO1994013580A1 (de) 1994-06-23
NO952097L (no) 1995-05-29

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